Treatment of normally gaseous mixtures



H. H. WENZKE TREATMENT OF NORMALLY GASEOUS MIXTURES Oct. 12, 1948.

2 Shee'ts-Sheet l Filed May 29, 1944 lrl )Kfer/Z651.-

ct, l2, i948. H. H. WENZKE TREATMENT OF NORMALLY GASEOUS MIXTURES 2 Sheets-Sheet 2 Filed May 29, 1944 Patented ct. 12, 1948 TREATMENT F NORMALLY GASEOUS MIXTURES Herman H. Wenzke, Chicago, Ill., assigner to Universal Oil Products Company, Chicago, Ill., a

corporation of Delaware Application May 29, 1944, Serial No. 537,934

Claims. l

This invention relates to the treatment of normally gaseous mixtures and more particularly to a method of separating individual gaseous fractions frorn a mixture also containing lighter and heavier components.

More specifically this invention involves the use of separation, absorption, and fractionating steps connected to function in an interdependent and cooperative manner with a resultant more eicient separation of individual fractions from mixtures of normally gaseous components than is obtainable in equipment now in general use when operated in a conventional manner.

Broadly, the invention comprises a process for separating a desired gaseous fraction from a mixture also containing lighter and heavier components which comprises commingling said mixture with a liquid absorbent under superatmospheric pressure and at a temperature sufficiently lovv that said desired gaseous fraction and a small amount of lighter gases are retained in said liquid absorbent, separating the resultant rich absorbent from 'the undissolved gases, stripping the lighter gases from the rich absorbent, and combining the stripped lighter gases with said mixture and said liquid absorbent prior to said cooling, and fractionating said stripped rich absorbent to separate the desired gaseous fraction therefrom.

In a more specic embodiment the invention comprises a process for separating a gaseous hydrocarbon from a hydrocarbon mixture also containing lighter and heavier components which comprises commingling said hydrocarbon mixture with a liquid absorbent under superatmospheric pressure and at a temperature sufficiently low that said desired gaseous hydrocarbon and a small amount of lighter gases are retained in said liquid absorbent, separating the resultant rich absorbent from the undissolved gases, stripping the lighter gases from the rich absorbent and combining the stripped lighter gases with said hydrocarbon mixture and said liquid absorbent prior to said cooling, and fractionating said striped rich absorbent to separate the desired gaseous hydrocarbon therefrom.

At the present time normaly gaseous materials, particularly normally gaseous hydrocarbons are employed4 as starting materials for the synthesis of many organic compounds. For example, ethylene is in great demand for many processes, it being employed as the starting material for the production of alcohol useful in the manufacture of explosives and as a starting material for the manufacture of butadiene. Ethylene as Well as various other gaseous olens including propylene and butylenes are useful as starting materials for various alkylation and polymerization processes for the manufactuer of motor fuels of exceptionally high antiknock quality.

Heretofcre, processes for the separation of individual hydrocarbons from the gaseous products of hydrocarbon cracking and conversion processes, such as thermal cracking and reforming or catalytic cracking and reforming processes, have not been of commercial practicability. rl'he present invention offers an efficient process for the separation of individual hydrocarbons or narrow boiling range fractions of gaseous hydrocarbons from normally gaseous hydrocarbon mixtures also containing lighter and heavier components than the fraction which is desired.

In order to further illustrate the features and advantages of the present invention, reference is made to the accompanying diagrammatic drawing and the following description thereof:

Figure 1 illustrates one specific form of apparatus in which the process of the invention may be successfully conducted.

Figure 2 illustrates another form of apparatus in which the process of the invention may be successfully conducted.

In connection With the explanation of the operation of equipment shown in Figure 1, the description will be limited to obtaining ethylene as the desired hydrocarbon from a gaseous hydrocarbon fraction. It is to be understood, however, that any other desired hydrocarbons or narrow boiling range hydrocarbon fractions may be separated from hydrocarbon mixtures containing lighter and heavier materials by adjusting the operating conditions of the apparatus.

Referring to Figure l, a normally gaseous hydrocarbon mixture comprising substantially hydrocarbons boiling below butane is introduced through line l at a suitable pressure depending upon the operating temperature of the separating equipment. Lean gases produced as hereinafter described are conducted through line 2 and commingled with the normally gaseous hydrocarbons in line l along with a liquid absorbent conduced through line 3 and produced as hereinafter described. The resultant mixture is then cooled in cooler 4 to a temperature below the critical temperature of ethene which is about 49 F. at a pressure sufficient to liquefy ethane. For instance, this temperature when operating at 500 lbs. per square inch Would normally be about 20 F. On the other hand, when operating at Vabout 250 lb-s. per square inch, this temperature would necessarily be about 20 F. The cooled mixture in line I is then directed into separation Zone wherein the liquid absorbent and hydrocarbons dissolved therein are separated from the unabsorbed gases. The rich liquid absorbent containing dissolved hydrocarbons is Withdrawn from separation zone 5 by means of line 6 and pump 1 wherefrom it is conducted by line 8 to stripper 9. In stripper 9, substantially all of the hydrocarbons boiling below ethylene are removed from the rich liquid absorbent and returned through line 2 to line l as the aforesaid lean gases. Heat for stripping may be supplied to stripper 9Y by any conventional means such as reboiler I9.

It is, of course, within the scope of the invenreiiux therefor.

4 withdrawn from the upper portion of absorber 31 by means of line 43 to be commingled with the lean liquid absorbent in line 33 thereby providing an added reflux for the column. Heat may be removed from an intermediate point in absorber 31 by means of `pump 44 and cooler 45, which are interposed in recycle line Y4t,

The ethylene-ethane mixture removed as an overhead product from fractionator IB is directed through line 41 to condenser 48 wherefrom the cooled mixture is directed by means of line k49 to receiver 50. In receiver 50, the condensed distillate is separated from the gaseous material and returned by means of line 5I containing pump 52 to the upper portion of fractionator I8 to act as drawn from receiver 5D by means of line 53 and stripped rich liquid absorbent substantially free from dissolved hydrocarbons boiling lower than Aby means of a suitable heating medium supplied n thereto and withdrawn therefrom by means of lines 22 and 23 respectively. The lean liquid absorbent containing substantially no ethane or lower-boiling hydrocarbons is withdrawn` from reboiler I9 through line 24 to be cooled in cooler 25 wherefromit is directed through line 26 containing valve 21 to a flash separation vessel 28. The pressure of the cooled liquid medium passing through valve 21 is reduced and the heat contained therein is sufficient to vaporize someof the lighter hydrocarbon components which are removed from vessel 28 by line 29 controlled by valve 3i! to be supplied to the plant fuel gas systemor used for any other purpose to which they may be suited. Unvaporized liquid is removed vfrom vessel 28 by means of line 3|' and pump 32 from which the liquid absorbent is directed through line 33 containing heat exchanger 34 to condenser 35. Y

. YThe above mentioned unabsorbed gases in separation vessel 5 are removed therefrom through line 35 and directed into absorber 31.

YThe lean liquid absorbent, after being cooled in moved from the system through line 4I controlled by valve 42. Some vaporous hydrocarbons are to commingle in line 53 with the chargingmate-Y rial to fractionator 54.`

The overhead product from fractionator 54 is removed therefrom by means of line 59 and cooled in condenser $0. The resultant cooled products are then directed by means of line 6I to receiver 52, wherefrom the uncondensed gases comprising a substantial portion of ethylene are removed through line 63 controlled by valve 34. The condensed distillate is removed from receiver 62 by means of line 65 containing pump 55 and supplied to the top of fractionator 54 to act as reflux therefor.V The required heat of vaporization is supplied to fractionator 55 by means of reboiler 61 connected thereto by lines 38 and 69. Reboiler 51 is heated by any suitable heating medium supplied thereto and withdrawn therefrom by means of lines 10 and ,'II respectively.

The liquid product from the bottom of fractionator 55 is removed from reboiler B1 through line 12 containing Valve 13. Valve 13 is regulated to cause the expansion of the liquid product from fractionator 55, thereby causing a considerable reduction in its temperature. This relatively low temperature material is then directed to heat exchanger 34 wherein it is passed in indirect contact and heat exchanger relationship with the aforesaid liquid medium carried by line 33 thus cooling the same. After passing through heat exchanger 34, the material in line 12 may be directed to the fuel gas system for the plant or it may be put to -any'other suitable use.

Excess liquid absorbent may be removed from ile system through line 14 controlled by valve Referring now to Figure 2, in this particular modification of the invention the process of the invention is applied tothe fractionating step in which the desired component is separated from the liquid absorbent.

VA gaseous hydrocarbon mixture is introduced Vto the system under pressure by means of line BI).V

In line 8U this `material is contacted with lean gases passing through lineSI and with ar liquid absorbent passing through line 82. The chargeV together with the lean gas and liquid absorbent pass into cooler 83 in which theVV conditions of temperature and pressure are so maintainedr as someV of the lighter components to become sub-` The gaseous material is with-V to cause the desired component in the charge and ala-:since .s v'stantially liquefied and dissolved in the liquid absorbent. The 'cooled material then passes throughf line 04 into f separator 1 B5. In separator "85'therichliquid absorbent containing dissolved gases Yis separated :from the undissolvedgases,

the latter passing through line 8B into absorber "87. Therich liquid absorbent is Witl-idrawn from separator -85 through line `8B vandfpurrip Bil-'and bdirected into stripper 30. Stripper-901soperated lunder conditions of temperature and pressure such'that the dissolved gases -lig'hter than lthe :desired-fraction are stripped from the rich liquid .absorbent andpassed through line 8| to becommingled with the charge inline 80.

.In order to maintain the desired temperature zini'fstripper 90, heat is supplied thereto bylmean-s :of reboiler 9| which is interconnected with the column by means of lines 92 and |33. Afsuitablc heating medium may be supplied and withdrawn from reboiler 9| by means of lines 94 and 95, frespectively.

The rich liquid absorbent stripped of lighter gases 'but 'still retaining the "desiredracti'on is 'withdrawn-from reboilerl by means of 4'line 93 "and pump "91 'and Acommingled With Ya :second liquid-"absorbent passing through line 193 anda `second'lean gas passing `through line 99. L'Ihe liquid absorbent containing the desired fraction plus the second liquid absorbent and second lean gas passinto'cool'er |00'Wherein'the temperature Yandpressure are maintained Ysuch V'thatthe desired component 'is niet substantially retained `in the combined liquid Vabsorbent. The cooled material'is'then'passed'bymeans'of line |0| into separator 92. In lseparator I 02 'thedesired iracti'on Vis separated from vthe combined'llquid "absorbent as a gas Varid'passed through line|03 into absorber |04. The rich combined liquid absorblent is withdrawn from separator |02 by means of line and pump |05 and directediinto stripper |01. Stripper |01 is maintained at conditions of temperature and pressure such thatv any of the desired fraction remaining in the rich combined liquid absorbent is removed therefromgand passed foverhead by means of line 99 `as said second lean lgas.

VAny of the desired fraction passing into ab vsorber y81 is absorbed fromv the lighter gases by 'means of liquid absorbent introduced through line |08. The'thus enriched liquid absorbent is then withdrawn'from the bottom of the absorber bymeans of line B2 and pump'l09. The lean gases lighter than the desired lfraction are removed from the system through line :i |0 controlled .by valve Iii. In this particularfabsorberan intercooler H2 is employed which is connectedito the column by means of lines H3 and H54. .Circula- .tion through cooler ||2 ismaintained bymea'ns of pump |5.

In absorber |04 those components higherboiling than the desired'fraction are absorbedin a liquid absorbent introduced through line H5. vThe thus enriched absorbent is then `Withdrawn vby means of pump ||'l and. line 98 as said second liquid-absorbent. The desired fraction is withdrawn from the system through line ||`8 controlled by valve H9. The desired temperatureis maintained in absorber |04 by lmeans of cooler |.20,-connectlng lines'i2 and |22, and circulating pump |23.

Stripper ii'l is supplied with the necessary heat-by means of reboiler |24'Whch isiconnected f l.therewith by means of lines |25 and |25. I-Ieat `is supplied to thereboiler by means ofv a suitable '.heatt convectiveflui'd supplied to and lwithdrawn lfrom the reboilerbylines 121 and respeo'- tively. "Tl-ie l combined lliquid .absorbent stripped of "the Adesired fraction and lighter gases @passes vthrough-line "|29an'd cooler i 30 into stripper 51131.

vStripper I3! v*is supplied with the fnecessary fheat i by'vmeans `of reboilerf 32 connected therewithby means of line |33 and if 34. Heat :iis supplied itc reboiler |32 f by -a sui-table' convectiveheating iluid passing throug'hllines t3-15 and |36. Inistripper |131 the-'heavier componentsfoflthe chargeimaybe "separated from'theonee strippedfcombined liquid absorbent. This l:stripped 4r-natei"ial ipasses roverhea-d throughl line f F31 vinto condenser $38. The resultant 'cooled fmateria'l is Althen fseparated iin receiver A"I3-9. `The stripped gases `are .removed -from 'the system by'means f'f line |340 "controlled passed by means vof line [412 'vfan'd pump @F43 iinto line |20 to'bef commingledwithithef chargelto lthe stripper. 'I'his distillate will ingenerabcompr-ise componentsL of theliquid absorb entfwhich 'passed overheadffromfthestripperandmay-fcontainssmall percentages of the *heavier -cOmponents Ldf 'Dthe 1 charge :to the plant. The lean liquid `absorbent is Withdrawn from `reboiler l |32 `by y"means "df "line A.Hill and passes through cooler |45 into surge drum A46. From surge drum |46 the lean liquid ab .sorbent'is directed by means of pumpf 41 and'line The following examples-@are included to illustrate the utility of this invention:

.Example ITI In equipment such as thatsshown 1in I'Figure "1 a normally gaseous hydrocarbon feed having an :analysis .as `shown `in the Afollowing table :is

vcharged `-to the plant through -line ata '-pres- "Mlpencent .Hydrogen 1'52 .'Methane T2750 -"Ethylene .1'0L4 '.Ethane @11528 llPropylene-i- 41.6

' This material is .commingled Vwith .a liquid absorbent returned through line 3 and lean gases `:returned through line 2 and the mixture cooled in cooler 4 to a temperature of about 20 F., the pressure vbeing lsubstantially 500 ipoun'ds per squarev inch. `The' liquidv componentfrom 'separator'5 is'directed to "stripperifS which is-'Voperated With'a wtop temperature'of 4abouteO Ffandat'a the `-bottom temperature vo'i stripper 9 at "about pressure of abouti510 `poundspersquare inch. 'Reboiler I0 provides heat -suiicent to "maintain "137 F. Thef-liquid vr'fraction from "stripper 911s lthen -:directed to ifractionator ='|"8 "which is operated at about '510 pounds per square inch pressure with fa'topf'temperature of yabout f100`fFfand bottom temperature of fractionator 55 being maintained at about 103 F. and the top temperature of fractionator 54'being maintained at about 22 F. The bottoms from fractionator I8 is'passed through cooler 25 and pressure reducing valve 21 wherein aV portion thereof is ashed thus reducing the temperature from about 100 F. to about 58 F. The unlashed material is then directed by meansof line 3l, pump 32, and line 33 through heat exchangerv 34, condenser 35 and line 38, into absorber 37. The bottoms from fractionator 55 areflashed by flowing through reducing valve 13 inline l2 and then passed in indirect heat exchange relation with the uniiashed bottoms from fractionator i8 in heat exchanger 34. .l

The bottoms from fractionator 55, after flashing, will have a temperature of about F. This material in heat exchanger 34 will reduce the temperature of the unilashed bottoms from fractionator, i8 to about 20 F.

The overhead product from fractionator 54 is cooled in condenser 60 and the uncondensed material removed from the system by means oi line 63 controlledrby valve 64. This material has an analysis as shown by the following table:

' l Mol per cent Methane Ethylene 95.0 Ethane These data indicate that approximately 90% of the original ethylene charged to the system is recovered in a fraction which is comprised of about'95% pure ethylene.

Example II This example employs theequipment of Figure 1 and a charge having an analysis as shown in the following table: g

.This material is -comrningled in1 line I withi-a liquid absorbent from line 3 and lean gases from line2 and cooled in cooler l to a temperature of about 100 F. at a pressure of about 200 pounds per square inch. IThe richVv liquid absorbent from separator 5 is directed to stripper 9 which is operatedrat a top temperature of about-145 `F .and a pressure of about 200 pounds per square inch. The bottom temperature yof stripper 9 is maintained ata temperature Yof about 250 F. The liquid fraction from stripper 9 isthen directed to fractionator i3 whichmisfoperated at about 140 pounds per square inch with a top temperature 'oi about 140 E'. and a bottom temperature kof about 360 F. i' Thev overhead product VVVfrom fractionator 1 8 *thenY treated in iractionas l Mol per cent Ethylene 0.1 Ethane 4.8 Propylene 34.7 Propane 59.7 Butylenes 0.2 i-Butane 0.4 n-Butane 0.1

These data indicate that a propane-propylene fraction of better than 94% purity is readilyk obtainable when employing the present invention. In this example the material passing through line 12 has an analysis as shown in the following table:

Mol per cent Propylene 0.9 Propane 1.5 Butylenes 30.2 i-Butane 46.2 n-Butane 20.2 i-Pentane 0.7 n-Pentane 0.1. Pentenes 0.2

These data indicate that a butane-butylene fraction of better than 96% purity is also obtainable in the same operation, when employing the present invention.

The above examples clearly demonstrate the very eflicient means which the present invention provides for the separation of individual hydrocarbons and hydrocarbon fractions fromhydrocarbon mixtures also containing lighter and heavier components. These examples, however, are not to be construed as a limitation on the process because it is readily applicableV to the separation of gaseous materials other than hydro.- carbons and is only to be limited to theV extent of the limitations in the. appended claims.

I claim as my invention:

1. A proces-s for separating a desired gaseous fraction from a gas mixture alsol containing lighter and heavier components which comprises commingling said mixture with a liquid absorbent under superatmospheric pressure, coolingV the resultant mixture of gases and liquid absorbent to a temperature suiciently low that said desired gaseous fraction and a small amount of lighter gases are retained in said liquid absorbent, separating the resultant rich absorbent from the undissolved gases, comprising a vsmall amount of said desired gaseous fraction, stripping the lighter gases from the rich absorbent by heating andV fractionating the same, commingling the stripped lighter gases lwith said gas mixture and said liquid absorbent prior to said cooling, separating the `desired gaseous fraction from .the stripped rich absorbent, contacting the resultant lean absorbent with said undissolvedgasesina countercurrent absorption Azone to absorb theV small amount of said desired gaseous fraction therefrom, and supplying the resultant solution vas said liquid absorbent.

2. A process for separating a desired gaseous hydrocarbon fraction from a hydrocarbon mixture also containing lighter and heavier components which comprises commingling said hydrocarbon mixture with a liquid absorbent under superatmospheric pressure, cooling the resultant mixture of hydrocarbons and liquid absorbent to a temperature suciently low that said desired gaseous hydrocarbon fraction and a small amount of lighter gases are retained in said liquid absorbent, separating the resultant rich absorbent from the undissolved gases, comprising a small amount of said desired gaseous hydro'carbon fraction, stripping the lighter gases from the rich absorbent by heating and fractionating the same, commingling the stripped lighter gases with said hydrocarbon mixture and said liquid absorbent prior to said cooling, fractionating the stripped rich absorbent to separate the desired gaseous hydrocarbon fraction therefrom, contacting the resultant lean absorbent With said undissolved gases in a countercurrent absorption zone to absorb the small amount of said desired gaseous hydrocarbon fraction therefrom, and supplying the resultant solution as said liquid absorbent.

3. A process for sep-arating a desired gaseous hydrocarbon from a hydrocarbon mixture also containing lighter and heavier components which comprises commingling said hydrocarbonl mixture with a liquid absorbent under superatmospheric pressure, cooling the resultant mixture of hydrocarbons and liquid absorbent to a, temperature suii'iciently low that said desired gaseous hydrocarbon and a small amount of lighter gases are retained in said liquid absorbent, separating the resultant rich absorbent from the undissolved gases comprising a small amount of said desired gaseous hydrocarbon, stripping the lighter gases from the rich absorbent by heating and fractionating the same, commingling th-e stripped lighter gases with said hydrocarbon mixture and said liquid absorbent prior to said cooling, fractionaiting the stripped rich absorbent to separate the desired gaseous hydrocarbon therefrom, contacting the resultant lean absor-bent with said undissolved gases in a countercurrent absorption zone to absorb the small amount of said desired gaseous hydrocarbon therefrom, and supplying the resul-tant solution as said liquid absorbent.

4. The process of claim 2 further characterized in that said desired gaseous hydrocarbon fraction comprises pricipally C3 hydrocarbons.

5. The process of claim 2 further characterized in that said desired gaseous hydrocarbon fraction comprises principally C4 hydrocarbons.

HERMAN H. WENZKE.

REFERENCES CITED rIhe following references are of record in the le of this patent:

UNITED STATES PATENTS 

